Process for producing acrylic acid

ABSTRACT

A process for producing acrylic acid from propane and oxygen gas through a vapor-phase catalytic oxidation reaction, said process comprising conducting the reaction using as a catalyst a metal oxide containing metallic elements Mo, V, Sb, and A (provided that A is at least one element selected from the group consisting of Nb, Ta, Sn, W, Ti, Ni, Fe, Cr, and Co). The metal oxide is prepared by a process including specific steps (1) and (2). The metal oxide may be supported on a compound containing specific elements.

FIELD OF THE INVENTION

The present invention relates to a process for producing a catalyst foruse in processes for producing acrylic acid by vapor-phase catalyticoxidation of propane.

BACKGROUND OF THE INVENTION

Acrylic acid is generally produced by a two-step oxidation process whichcomprises catalytically reacting propylene with oxygen at hightemperature in the presence of a catalyst to produce acrolein and thencatalytically reacting the acrolein with oxygen.

In recent years, however, processes for producing acrylic acid frompropane through one-step oxidation are being studied in order to reducethe cost of acrylic acid production. The main subject in these studiesis to seek for catalysts which give acrylic acid in high yields.Oxidation reaction catalysts for obtaining acrylic acid from propane(hereinafter referred to as "catalysts for acrylic acid production")have been proposed.

Examples thereof include a Bi--Mo--V oxide (see U.S. Pat. No.5,198,580), an Mo--V--Te oxide (see JP-A-7-10801 and JP-A-6-279351), anMo--Sb--P oxide (see U.S. Pat. No. 4,260,822), a V--P--Te oxide (seeJP-A-3-70445 and Catal. Today, Vol. 13, 679 (1992)), and a Bi--Mo--V--Agoxide (see JP-A-2-83348). (The term "JP-A" as used herein means an"unexamined published Japanese patent application".)

Among the catalysts enumerated above, those with which acrylic acid isobtained in high yields are the Bi-Mo-V oxide and the Mo--V--Te oxide.In the references disclosing the former catalyst, there is a descriptionto the effect that acrylic acid can be produced in a yield of 5% with aselectivity of about 28%. In the references disclosing the lattercatalyst, there is a description to the effect that acrylic acid can beobtained in a yield of from 35 to 40% with a selectivity of from 55 to60%.

In general, the performance of a catalyst does not solely depend on thekinds and proportions of the constituent metals, but considerablydepends also on the valences and crystal structures of the constituentmetals. It is generally known that the valences and crystal structuresof constituent metals contained in catalysts vary depending on catalystproduction processes.

The aforementioned Bi--Mo--V oxide catalyst or Mo--V--Te oxide catalystfor acrylic acid production is also produced by a technique intended toimpart excellent catalytic performance. Specifically, the techniqueemployed for producing the catalyst comprises evenly mixing telluricacid, ammonium paramolybdate, ammonium metavanadate, or bismuthtriacetate, in a heated aqueous medium, evaporating the water to obtaina solid mixture, and calcining the solid mixture at 400 to 600° C. Atechnique known to be effective in enhancing catalytic performancecomprises mixing compounds of antimony, niobium, vanadium, andmolybdenum in a heated aqueous medium to obtain a slurry and mixing thisslurry with a separately prepared slurry containing a bismuth compoundand a molybdenum compound (see U.S. Pat. No. 5,198,580).

On the other hand, catalysts produced from a vanadium compound/antimonycompound mixture obtained through the reaction shown by the followingscheme (1) are known as catalysts not for the production of acrylicacid, but for producing acrylonitrile by oxidizing propane in thepresence of ammonia, i.e., as catalysts for the ammoxidation reaction ofpropane. Examples of these ammoxidation catalysts include a V--Sb metaloxide (see U.S. Pat. No. 5,498,588 and JP-A-2-180637) and an Mo--V--Sbmetal oxide (see JP-A-9-157241).

    V.sup.+5 +Sb.sup.+3 →V.sup.+3 +Sb.sup.+5            (1)

The above reaction is usually conducted using a compound of trivalentantimony, e.g., antimony trioxide, and a compound of pentavalentvanadium, e.g., ammonium metavanadate, in an aqueous medium at atemperature of 80° C. or higher.

However, reaction (1) shown above has not hitherto been employed forproducing a catalyst for acrylic acid production.

SUMMARY OF THE INVENTION

The present inventors made intensive investigations on one-stepprocesses for industrially advantageously producing acrylic acid frompropane. As a result, they have found that a catalyst containingmolybdenum, antimony, vanadium, oxygen, and one or more specific metalsas essential components is decreased in the deterioration of catalyticactivity and is capable of producing acrylic acid in high yield. Thepresent invention has been completed based on this finding.

The present invention provides, in the first embodiment thereof, aprocess for producing acrylic acid from propane and an oxygen-containinggas through a vapor-phase catalytic oxidation reaction, the processcomprising conducting the reaction using as a catalyst a metal oxidecontaining metallic elements Mo, V, Sb, and A (provided that A is atleast one element selected from the group consisting of Nb, Ta, Sn, W,Ti, Ni, Fe, Cr, and Co).

The present invention further provides, in the second embodimentthereof, a process for producing acrylic acid which comprises conductingthe reaction using as a catalyst a metal oxide obtained by depositing atleast one compound which contains an element B (provided that B is atleast one element selected from the group consisting of Na, K, Rb, Cs,P, and As) as a component thereof on the metal oxide used in the processaccording to the first embodiment described above and then burning theresulting mixture.

The present invention furthermore provides, in the third embodimentthereof, a process for producing a catalyst which is for use inproducing acrylic acid by gas-phase catalytic oxidation of propane andcomprises the metal oxide used in the process according to the firstembodiment described above, the process comprising the following steps(1) and (2):

step (1): reacting V⁺⁵ with Sb⁺³ in an aqueous medium at a temperatureof 70° C. or more in the presence of Mo⁺⁶ and, during or after thereaction, bubbling either molecular oxygen or a gas containing molecularoxygen into the reaction mixture; and

step (2): adding a compound containing the element A as a componentthereof to the reaction product obtained in step (1) above, mixing theingredients to obtain a homogeneous mixture, and burning the resultingmixture.

DETAILED DESCRIPTION OF THE INVENTION

The present invention is described in detail below.

The metal oxide used in the process according to the first embodiment ofthe present invention comprises metals comprising essential metallicelements Mo (molybdenum), V (vanadium), Sb (antimony), and A (providedthat A is at least one element selected from the group consisting of Nb,Ta, Sn, W, Ti, Ni, Fe, Cr, and Co; the same applies hereinafter) andoxygen. In this metal oxide, the proportions of those metals arepreferably represented by the following empirical formula (1):

    MoV.sub.i Sb.sub.j A.sub.k                                 (1)

(wherein i, j, and k each is preferably from 0.001 to 3.0, morepreferably from 0.01 to 2.0, most preferably from 0.1 to 0.5).

Preferred among the metals represented by A are Nb and Ta.

In the metal oxide described above, if the proportion of V to Mo exceeds3, combustion reaction is more apt to occur. If the proportion of Sb toMo exceeds 3, a decreased conversion of propane results. If theproportion of A to Mo exceeds 3, not only a decreased conversion butalso a decreased proportion of acrylic acid in the reaction products,i.e., a decreased selectivity, results. If the proportion of any of V,Sb, and A to Mo is below 0.001, the results are a poor conversion ofpropane and a poor selectivity for acrylic acid.

The proportion of oxygen in the catalyst is fixed by the valences of theelements Mo, Sb, V, and A.

The catalyst described above can be prepared by conventional methods.For example, the catalyst is produced as follows. First, solutions orsuspensions respectively containing various compounds containing Mo, Sb,V, and A ("A" has the same meaning as defined above) as components aremixed together in such a proportion that the atomic ratio among themetal components becomes a value within the range specified above.Although the compounds containing those metal components are notparticularly limited, preferred examples thereof include oxides,chlorides, hydroxides, ammonium salts, nitrates, and alkoxides.

Specific preferred examples thereof are as follows. Those metalcompounds may be used in a proportion corresponding to the metalliccomposition of the target oxide.

Mo: molybdic acid, ammonium molybdate, molybdenum oxide

V: vanadium oxide, ammonium metavanadate

Sb: antimony chloride, antimony acetate, antimony trioxide

Nb: niobic acid, niobium hydrogen oxalate, niobium oxide, niobiumchloride

Ta: tantalic acid, tantalum oxide, tantalum chloride, tantalum ethoxide

Sn: tin oxide, tin hydroxide, stannous chloride, stannic chloride, tinoxalate

W: tungsten oxide, tungstic acid, tungsten chloride, ammoniumparatungstate

Ti: ammonium titanium oxalate, titanium butoxide, titanium chloride

Ni: nickel nitrate, nickel oxalate, nickel chloride

Fe: iron nitrate, ferric chloride, iron hydroxide

Cr: chromium nitrate, chromium chloride, chromium oxide

Co: cobalt nitrate, cobalt acetate, cobalt hydroxide, cobalt chloride.

After compounds containing the metal components are mixed by the methoddescribed above, or the like, the mixture is dried and calcined in anordinary way to thereby obtain the target catalyst. Usable dryingmethods include ordinary drying techniques such as evaporation todryness, spray drying, and vacuum drying. On the other hand, thecalcination is desirably conducted in an inert gas stream, e.g.,nitrogen or argon. In such preferred calcination methods, thetemperature is preferably from 250 to 1000° C., more preferably from 350to 900° C. Although the calcination period is not particularly limited,it is preferably from 1 to 20 hours.

The catalyst for use in the process according to the first embodiment ofthe present invention can be used even in an unsupported state. However,the catalyst may comprise the aforementioned metal components fixed to asupport such as, e.g., silica, alumina, silica-alumina, or siliconcarbide. For fixing the metal components to these supports, knownmethods can be employed without particular limitations. For example, apreferred method comprises infiltrating a solution or suspension ofcompounds containing the aforementioned metal components into a supportand then drying and calcining the impregnated support by the methodsdescribed above.

The catalyst is not particularly limited in shape, size, particlediameter distribution, or the like, and can have any propertiesconcerning shape and size selected according to the structure of theacrylic acid synthesis reaction vessel to be used. Examples of thecatalyst shape include powder and molded forms such as granules,spheres, or solid or hollow cylinders.

After accomplishment of the invention described above, the presentinventors made intensive investigations for the purpose of obtaining acatalyst having even higher performance. As a result, the followingmethod was achieved.

Namely, the method achieved is a process for producing a catalyst whichis for use in producing acrylic acid by gas-phase catalytic oxidation ofpropane and comprises a metal oxide containing metallic elements Mo, V,Sb, and A (provided that A is at least one element selected from thegroup consisting of Nb, Ta, Sn, W, Ti, Ni, Fe, Cr, and Co). This processcomprises the following steps (1) and (2):

step (1): reacting V⁺⁵ with Sb⁺³ in an aqueous medium at a temperatureof 70° C. more in the presence of Mo⁺⁶ and, during or after thereaction, bubbling either molecular oxygen or a gas containing molecularoxygen into the reaction mixture; and

step (2): adding a compound containing the element A as a componentthereof to the reaction product obtained in step (1) above, mixing theingredients to obtain a homogeneous mixture, and calcining the resultantmixture.

This process is explained below in more detail.

In step (1) in this process, oxidation-reduction reactions occur amongthe three reactants, i.e., Sb⁺³, V⁺⁵, and Mo⁺⁶, in an aqueous medium ata temperature of 70° C. or higher. The main reaction of these reactionsis represented by the following scheme (A).

    V.sup.+5 +Sb.sup.+3 →V.sup.+3 +Sb.sup.+5            (A)

If Mo⁺⁶ is not present in the reaction system containing the threereactants, the following reaction is known to occur simultaneously withthe above reaction [see Studies in Surface Science and Catalysis, Vol.82, p. 281 (1994)].

    V.sup.+3 +V.sup.+5 →2V.sup.+4                       (B)

In contrast, in the above process according to the present invention, inwhich Mo⁺⁶ coexists, the V⁺³ formed by reaction (A) is rapidly oxidizedto V⁺⁴ by the Mo⁺⁶. As a result, reaction (B) is inhibited and, hence,most of the V⁺⁵ used participates in reaction (A).

Preferred examples of the V⁺⁵ compound which contains V⁺⁵ as aconstituent element and is used in the above-describedoxidation-reduction reaction in this process include ammoniummetavanadate and vanadium pentoxide. Preferred examples of the Sb⁺³compound containing Sb⁺³ as a constituent element include antimonytrioxide and antimony acetate. Examples of the Mo⁺⁶ compound containingMo⁺⁶ as a constituent element include ammonium molybdate, molybdenumoxide, and molybdic acid. Among these molybdenum compounds, ammoniummolybdate is preferred because it is water-soluble.

For the oxidation-reduction reaction, the Mo⁺⁶, V⁺⁵, and Sb⁺³ compoundsare used in such a proportion that the atomic ratio among the Mo, V, andSb contained in the target compound to be obtained will be representedby the empirical formula given below. The V⁺⁵ and Sb⁺³ compounds areused in such a proportion that the Sb⁺³ /V⁺⁵ atomic ratio is (0.3-1)/1.If the proportion of Sb⁺³ is below 0.3, a decreased selectivity foracrylic acid results. If the proportion thereof exceeds 1, a decreasedconversion of propane results.

The oxide contains Mo, V, Sb, and A in a proportion represented by thefollowing empirical formula (1):

    MoV.sub.i Sb.sub.j A.sub.k                                 (1)

(wherein i, j, and k each is from 0.001 to 3.0).

Preferably, A is Nb or Ta, and i and j each is from 0.01 to 1.5,provided that j/i is from 0.3 to 1. Especially preferably, i and j eachis from 0.1 to 1.

If i or j in the above empirical formula is below 0.01 or above 1.5, thereaction for producing acrylic acid results in a poor conversion ofpropane and a poor selectivity for acrylic acid.

The total feed amount of those three metal compounds is from 3 to 30parts by weight per 100 parts by weight of the aqueous medium. If thetotal amount of the three metal compounds exceeds 30 parts by weight,part of the vanadium compound or molybdenum compound remains undissolvedand the oxidation-reduction reaction is apt to proceed incompletely.

The reaction described above does not proceed at temperatures lower than70° C. Preferred reaction temperatures are around the boiling point ofthe aqueous medium. The reaction time is preferably about from 5 to 15hours.

The degree of progress of the reaction can be determined by determiningthe amount of pentavalent antimony present in the reaction mixture andcomparing this found value with the amount of the trivalent antimony fedinitially. Specifically, the amount of pentavalent antimony contained inthe reaction mixture obtained can be determined by adding 1 N aqueousoxalic acid solution to the reaction mixture in an amount at least 10times the amount of the reaction mixture to thereby precipitate theantimony only, and then titrating the precipitate with hydriodic acid.

The valences of the molybdenum and vanadium contained in the reactionmixture can be determined, e.g., by electron spin resonancespectrometry.

In this process, molecular oxygen (hereinafter referred to as "oxygengas") or a gas containing oxygen gas (inclusively referred to as"oxygen-containing gas") is bubbled into the oxidation-reductionreaction mixture as stated above. The bubbling of an oxygen-containinggas into the oxidation-reduction reaction mixture may be conductedeither during or after the oxidation-reduction reaction. During thebubbling of an oxygen-containing gas, the reaction mixture is preferablykept being stirred.

By bubbling an oxygen-containing gas into the oxidation-reactionmixture, a catalyst having high performance can be obtained as inExamples 10 and 11 described hereinafter.

The oxygen gas concentration in the oxygen-containing gas is preferably0.5 vol % or higher, more preferably from 1 to 20 vol %, and mostpreferably from 2 to 15 vol % (hereinafter abbreviated as %). If theoxygen-containing gas has an oxygen gas concentration lower than 0.5%,the catalyst finally obtained may have a decreased activity.

The preferred range of the rate of bubbling (flow rate) depends on theamount of the oxidation-reduction reaction mixture. When the amount ofthe reaction mixture is about from 200 to 500 ml, the rate of bubblingis preferably from 3 to 12 l/hr.

The period of the bubbling of an oxygen-containing gas into the reactionmixture is preferably 4 hours or longer, and more preferably from 5 to10 hours. If the period of bubbling of an oxygen-containing gas isshorter than 4 hours, the catalyst obtained may have a decreasedactivity.

As to how the molecular oxygen introduced by the bubbling of anoxygen-containing gas into the reaction mixture reacts with compoundspresent in the reaction mixture has not been elucidated. However, fromthe determination of Mo⁺⁵ in the reaction mixture, it has beenascertained that the Mo⁺⁶ which oxidizes V⁺³ to V⁺⁴ in the presentinvention is first reduced to Mo⁺⁵, part of which thereafter returns toMo⁺⁶ again. It is presumed from the above chemical changes that themolecular oxygen serves to oxidize the Mo⁺⁵.

In this process, the metal A (provided that A is at least one elementselected from the group consisting of Nb, Ta, Sn, W, Ti, Ni, Fe, Cr andCo) is added to either the dispersion which is the reaction mixtureresulting from the above reaction and contains molybdenum, vanadium, andantimony, or a solid matter obtained by subjecting the dispersion toevaporation to dryness. These ingredients are mixed together to give ahomogeneous mixture. The metal A preferably Nb or Ta. Examples of theniobium or tantalum compound include niobium oxide, niobic acid,tantalum oxide, and tantalic acid. Although the niobium or tantalumcompound may be used as an aqueous dispersion thereof, the compound ispreferably used in the form of an aqueous solution of, e.g., thecorresponding oxalate prepared by using oxalic acid.

The niobium or tantalum compound is used in such an amount as to give acatalyst in which the atomic ratio of niobium or tantalum to molybdenumis (0.001-3.0)/1. If the proportion of niobium or tantalum to molybdenumin the catalyst obtained is below 0.001/1, this catalyst deteriorates.If that proportion exceeds 3.0, the catalyst has low activity and areduced conversion of propane results.

The mixture of metal compounds obtained through the procedure describedabove is burned, if necessary after being dried by evaporation todryness, spray drying, etc. The mixture is thus converted to the metaloxide to be used as a catalyst in the present invention.

The calcination can be conducted under conditions generally employed forthe production of metal oxide catalysts. Specifically, the calcinationconditions preferably include a temperature of from 300 to 900° C. and acalcination period of from 1 to 20 hours, and more preferably include atemperature of from 450 to 700° C. and a period of from 1 to 2 hours.Where an oxalate was added as the fourth metal compound after thepreparation of a mixture comprising compounds of molybdenum, vanadium,and antimony, the calcination is especially preferably conducted firstat around 300° C. for about 5 hours and then at around 600° C. for about2 hours. The atmosphere for calcination is preferably an inert gasstream, such as nitrogen or argon, or air. More preferred is the inertgas stream because a catalyst having higher activity is obtainabletherewith.

The metal oxide obtained by the process described above was analyzed byX-ray powder diffractometry (X-ray source: Cu--K.sub.α line). Theresults obtained were compared with those for a metal oxide obtained byconducting the same procedure as the above except that the bubbling ofan oxygen-containing gas during the heating of the compounds ofmolybdenum, vanadium, and antimony in an aqueous medium was omitted. Thecomparison revealed that the relative intensity of the peak at adiffraction angle 2θ of 28.1 for the metal oxide according to theinvention was about 1/2 to 1/3 of that for the other metal oxide,showing that the two oxides differed in crystal structure.

The contents of metal elements in the metal oxide obtained through theburning can be ascertained by fluorescent X-ray spectrometry.

In using the thus-obtained composite metal oxide as a catalyst foracrylic acid production, the oxide is preferably pulverized to anappropriate particle size to increase the surface area thereof. For thepulverization, either a dry or a wet method can be used. Examples ofusable pulverizers include mortars and ball mills. The particle size ofthe catalyst is preferably 20 jm or smaller, and more preferably 5 μm orsmaller.

In the process according to the second embodiment of the presentinvention, a compound containing an element B (B is at least one elementselected from the group consisting of Na, K, Rb, Cs, P, and As; the sameapplies hereinafter; this compound is referred to as "compound B") as acomponent thereof is deposited on the oxide obtained above (hereinafterreferred to as "supporting oxide"). The deposition amount of thecompound B is preferably from 0.001 to 0.3, and more preferably from0.002 to 0.1, in terms of the atomic ratio of the element B to themolybdenum contained in the supporting oxide. If the atomic ratio of theelement B to molybdenum is below 0.001, a decreased selectivity foracrylic acid results. If that atomic ratio exceeds 0.3, a decreasedconversion of propane results because the active surface of thesupporting oxide is covered with an oxide of the element B.

Examples of the compound B include sodium compounds such as sodiumcarbonate, sodium hydrogen carbonate, sodium hydroxide, sodium nitrate,and sodium oxide; potassium compounds such as potassium hydroxide,potassium hydrogen carbonate, potassium carbonate, potassium nitrate,potassium acetate, and potassium oxide; rubidium compounds such asrubidium hydroxide, rubidium carbonate, rubidium nitrate, and rubidiumoxide; cesium compounds such as cesium oxide, cesium carbonate, cesiumacetate, cesium hydroxides, and cesium nitrate; phosphorus compoundssuch as phosphoric acid, phosphorus oxide, and diammonium hydrogenphosphate; and arsenic compounds such as arsenic chloride, arsenictrioxide, and arsenic pentoxide. Preferred among the elementsrepresented by B are K, Rb, and P.

A preferred method for depositing a compound B on the supporting oxidecomprises mixing a solution prepared by dissolving the compound B inwater or an organic solvent such as alcohol with a powder of thesupporting oxide. The concentration of the compound of B in the solutionis preferably from 0.1 to 1.0 mol/l. The amount of the solution ispreferably from 20 to 50 parts by weight per 100 parts by weight of thesupporting oxide.

After the solution of the compound B is mixed with the powder of thesupporting oxide, the mixture is stirred to homogenize the same as muchas possible. The solvent in the resulting mixture is vaporized, e.g., byevaporation to dryness, whereby a metal oxide powder having the compoundB deposited thereon can be obtained. Calcining the thus-obtained metaloxide powder at 300 to 500° C. for 1 to 5 hours gives the target metaloxide for use as a catalyst.

The thus-obtained oxide having a compound B fixed thereto can be usedeven in an unsupported state. The oxide can also be used after beingfixed to a support having an appropriate particle size, such as silica,alumina, silica-alumina, or silicon carbide.

In the processes for producing acrylic acid according to the presentinvention, the starting materials, i.e., propane and anoxygen-containing gas, are introduced simultaneously into a reactor andreacted with each other in the presence of the catalyst. It is alsopossible to introduce propane and an oxygen-containing gas into areactor either separately or as a mixture thereof prepared beforehand.

A commercial propane as such can be utilized as the starting propanewithout subjecting the commercial product to a special treatment.However, the purity of the propane is desirably as high as possible,from the standpoint of inhibiting side reactions, etc. Examples of theoxygen-containing gas as the other starting material include air, oxygengas, and gaseous mixtures obtained by diluting these with an inert gassuch as, e.g., nitrogen, steam, or carbon dioxide. However, air isoptimal from the standpoints of safety and cost.

The mixing ratio between the propane and the oxygen-containing gas isnot particularly limited. However, where the oxygen-containing gas foruse in the reaction is air, the amount thereof is preferably up to 30times by volume the amount of the propane, and more preferably in therange of from 0.2 to 20 times.

Reaction systems of different catalyst packing types can be utilizedwithout particular limitations. Examples thereof include fixed-bed,moving-bed, and fluidized-bed systems.

Reaction conditions are not particularly limited. However, the reactiontemperature is preferably from 300 to 600° C., and more preferably from350 to 500° C. The reacting mixture gas is preferably fed at a spacevelocity (hereinafter referred to as "SV") of from 300 to 5,000 hr⁻¹.

In the production of acrylic acid from propane, the reaction yieldsby-products such as, e.g., propylene, carbon monoxide, carbon dioxide,and acetic acid besides acrylic acid as the target compound. Theseby-products can be separated from the acrylic acid by a purificationoperation based on differences in boiling point, e.g., distillation.Among the by-products, the isolated propylene, which serves as anintermediate for acrylic acid, can be utilized again in the reactionafter being mixed with feedstock propane. In this case, however, thepropylene is desirably mixed in an amount up to 20 vol % based on thepropane so as to avoid adverse influences on the reaction.

The present invention will be explained below in more detail byreference to Examples and Comparative Examples, but the invention shouldnot be construed as being limited to these Examples.

EXAMPLE 1

Into a 500-ml glass flask was introduced 259 ml of distilled water.Thereto was added 12.3 g of ammonium metavanadate. This mixture washeated with stirring to dissolve the salt. Thereafter, 12.7 g ofantimony trioxide was added, and this mixture was heated with ref luxingfor 12 hours. To the resulting mixture were successively added 61.0 g ofammonium molybdate and a solution prepared by dissolving 26.3 g ofoxalic acid and 6.5 g of niobic acid in 180 ml of distilled water withheating at 50° C. This mixture was stirred at 50° C. for 30 minutes. Theslurry thus obtained was concentrated by heating, dried at 120° C. for 3hours, and then calcined in a nitrogen stream at 600° C. for 2 hours toobtain a catalyst in which the Mo/Sb/V/Nb atomic ratio was1.0/0.25/0.3/0.1. The catalyst obtained was pulverized to 16- to 30-meshparticles. Thereafter, a 1.5 g portion (volume: 1.5 ml) of the particleswas packed into an 8-mmφ reaction tube made of quartz. A mixed gascomposed of 4.4 vol % propane, 7.0 vol % oxygen, 26.3 vol % nitrogen,and 62.3 vol % steam was fed to the reaction tube at an SV of 1,800 hr⁻¹to react the mixed gas at a temperature of 400° C. for 10 hours. Theresults obtained are shown in Table 1 below. The conversion of propane(%) and the selectivity for acrylic acid (%) shown in Table 1 werecalculated using the following equations (from the number of moles ofeach compound).

Conversion of propane (%)

=[(propane fed)-(unreacted propane)]/(propane fed) Selectivity foracrylic acid (%)

=(acrylic acid yielded)/[(propane fed)-(unreacted propane)]

In the catalyst composition shown in Table 1, symbol X, which indicatesthe proportion of oxygen, is fixed by the valences of the otherelements.

EXAMPLE 2

Using the same catalyst as in Example 1, reaction was conducted underthe same conditions as in Example 1, except that the reactiontemperature was changed to 410° C. The results obtained are shown inTable 1 below.

EXAMPLE 3

Using the same catalyst as in Example 1, a mixed gas composed of 4.4 vol% propane, 7.0 vol % oxygen, 57.6 vol % nitrogen, and 31.0 vol % steamwas reacted for 10 hours under the conditions of an SV of 1,800 hr⁻¹ anda temperature of 380° C. The results obtained are shown in Table 1below.

EXAMPLE 4

Into a 500-ml glass flask was introduced 259 ml of distilled water.Thereto was added 12.3 g of ammonium metavanadate. This mixture washeated with stirring to dissolve the salt. To this solution weresuccessively added 26.0 g of antimony acetate, 61.0 g of ammoniummolybdate, and a solution prepared by dissolving 26.3 g of oxalic acidand 6.5 g of niobic acid in 180 ml of distilled water with heating. Thismixture was stirred at 50° C. for 30 minutes. The subsequent procedurewas conducted in the same manner as in Example 1 to prepare a catalystin which the Mo/Sb/V/Nb atomic ratio was 1.0/0.25/0.3/0.1. The catalystobtained was pulverized to 16- to 30-mesh particles. Thereafter, a 1.5 gportion (volume: 1.5 ml) of the particles was used to react a mixed gascomposed of 4.4 vol % propane, 7.0 vol % oxygen, 26.3 vol % nitrogen,and 62.3 vol % steam for 10 hours under the conditions of an SV of 1,800hr⁻¹ and a temperature of 380° C. The results obtained are shown inTable 1 below.

COMPARATIVE EXAMPLE 1

Into a 500-ml glass flask was introduced 259 ml of distilled water.Thereto was added 12.3 g of ammonium metavanadate. This mixture washeated with stirring to dissolve the salt. To the resulting solutionwere successively added 61.0 g of ammonium molybdate and a solutionprepared by dissolving 26.3 g of oxalic acid and 6.5 g of niobic acid in180 ml of distilled water with heating. This mixture was stirred at 50°C. for 30 minutes. The slurry thus obtained was concentrated by heating,dried at 120° C. for 3 hours, and then burned in a nitrogen stream at600° C. for 2 hours to obtain a catalyst in which the Mo/V/Nb atomicratio was 1.0/0.3/0.1. The catalyst obtained was pulverized to 16- to30-mesh particles. Thereafter, a 1.5 g portion (volume: 1.5 ml) of theparticles was packed into an 8-mmφ reaction tube made of quartz, andreaction was conducted under the same conditions as in Example 1. Theresults obtained are shown in Table 1 below.

COMPARATIVE EXAMPLE 2

A catalyst was prepared in the same manner as in Comparative Example 1,except that 21.1 g of copper nitrate was additionally added. In thiscatalyst, the Mo/Cu/V/Nb atomic ratio was 1.0/0.25/0.3/0.1. Using thethus-obtained catalyst, reaction was conducted in the same manner as inExample 1. The results obtained are shown in Table 1 below.

COMPARATIVE EXAMPLE 3

A catalyst was prepared in the same manner as in Comparative Example 1,except that 42.2 g of bismuth nitrate was additionally added. In thiscatalyst, the Mo/Bi/V/Nb atomic ratio was 1.0/0.25/0.3/0.1. Using thethus-obtained catalyst, reaction was conducted in the same manner as inExample 1. The results obtained are shown in Table 1 below.

                                      TABLE 1                                     __________________________________________________________________________                                     Reaction                                                                           Conversion                                                                          Selectivity                         Catalyst Feedstock composition (vol %) SV tempera- of propane for                                                       acrylic                             composition propane/oxygen/nitrogen/steam (hr.sup.-1) ture (°                                                    C.) (%) acid (%)                  __________________________________________________________________________    Example 1                                                                           MoSb.sub.0.25 V.sub.0.3 Nb.sub.0.1 O.sub.x                                              4.4/7.0/26.3/62.3                                                                           1800                                                                             400  30.9  29.5                                Example 2 MoSb.sub.0.25 V.sub.0.3 Nb.sub.0.1 O.sub.x 4.4/7.0/26.3/62.3                                                  1800 410 34.1 23.3                  Example 3 MoSb.sub.0.25 V.sub.0.3 Nb.sub.0.1 O.sub.x 4.4/7.0/57.5/31.2                                                  1800 380 19.3 21.1                  Example 4 MoSb.sub.0.25 V.sub.0.3 Nb.sub.0.1 O.sub.x 4.4/7.0/26.3/62.3                                                  1800 380 21.5 6.8                   Comparative MoV.sub.0.3 Nb.sub.0.1 O.sub.x 4.4/7.0/26.3/62.3 1800 400                                                   21.1 0.8                            Example 1                                                                     Comparative MoCu.sub.0.25 V.sub.0.3 Nb.sub.0.1 O.sub.x 4.4/7.0/26.3/62.3                                                 1800 400 30.0 0.3                  Example 2                                                                     Comparative MoBi.sub.0.25 V.sub.0.3 Nb.sub.0.1 O.sub.x 4.4/7.0/26.3/62.3                                                 1800 400 21.0 2.                   Example 3                                                                   __________________________________________________________________________

EXAMPLE 5

To 130 ml of distilled water placed in a 300-ml glass flask was added6.15 g of ammonium metavanadate. This mixture was heated with stirringto dissolve the salt. Thereto were added 6.35 g of antimony trioxide and30.5 g of ammonium molybdate. An air/nitrogen mixed gas having an oxygengas concentration of 15% was bubbled into the resultant liquid mixtureat a flow rate of 100 ml/min while stirring the mixture with a stirrerat 360 rpm at an elevated temperature of 92° C. Thus, the mixture wasreacted for 5 hours.

The resulting blue colloidal dispersion was cooled to room temperature.An aqueous solution which had been prepared by dissolving 13.15 g ofoxalic acid and 3.25 g of niobic acid in 90 ml of distilled water andhad ordinary temperature was added to the dispersion. This mixture wasvigorously agitated for 30 minutes, concentrated by heating, and thensubjected to evaporation to dryness at 120° C.

The solid thus obtained was calcined in a nitrogen gas stream at 600° C.for 2 hours to obtain a metal oxide catalyst. Atomic ratio in this metaloxide was Mo/Sb/V/Nb=1.0/0.25/0.3/0.12.

To 5.0 g of the metal oxide obtained above (hereinafter referred to as"oxide a") was added a solution prepared by dissolving 0.030 g ofpotassium hydrogen carbonate in 1 g of distilled water. After thismixture was sufficiently mixed, it was dried at 120° C. for 1 hour andthen calcined at 350° C. for 2 hours to obtain a catalyst. The catalystwas pulverized to 16- to 30-mesh particles and packed into a reactor.

The catalyst obtained was examined by fluorescent X-ray spectrometry. Asa result, the Mo/Sb/V/Nb/K atomic ratio therein was found to be1.0/0.25/0.3/0.12/0.013.

A mixed gas composed of 4.4 vol % propane, 7.0 vol % oxygen, 26.3 vol %nitrogen, and 62.3 vol % steam (hereinafter referred to as "test gas")was fed to the reactor at an SV of 1,600 hr⁻¹ while maintaining thetemperature of the reactor at 400° C. The conversion of propane,selectivity for acetic acid, selectivity for propylene, and selectivityfor acrylic acid in the above reaction were calculated respectivelyusing the following equations. The results obtained are shown in Table 2below.

EXAMPLE 6

Reaction was conducted under the same conditions as in Example 5, exceptthat the reaction temperature was changed to 420° C. The results of thereaction are shown in Table 2 below.

EXAMPLES 7 AND 8

Catalysts were produced in the same manner as in Example 5, except thatin place of potassium hydrogen carbonate, each of the metal compoundsshown in Table 2, i.e., diammonium hydrogen phosphate (use amount: 0.03g) and rubidium nitrate (use amount: 0.044 g), was fixed to the oxide"a". Reaction was conducted in the same manner as in Example 5, exceptthat each of the catalysts thus obtained was used. The results obtainedare shown in Table 2 below.

EXAMPLE 9

To 5.0 g of the oxide "a" obtained in Example 5 was added a solutionprepared by dissolving 0.030 g of potassium hydrogen carbonate in 1 g ofdistilled water. After this mixture was sufficiently mixed, it was driedat 120° C. for 1 hour. Thereto was added a solution prepared bydissolving 0.040 g of diammonium hydrogen phosphate as the secondingredient in 1 g of distilled water. After this mixture wassufficiently mixed, it was calcined at 350° C. for 2 hours.

The catalyst thus obtained was pulverized to 16- to 30-mesh particlesand packed into a reactor. The test gas described above was reactedunder the conditions of a temperature of 400° C. and an SV of 1,600hr⁻¹. The results obtained are shown in Table 2 below.

                                      TABLE 2                                     __________________________________________________________________________                  Conversion                                                                          Selectivity for                                                                      Selectivity for                                                                      Selectivity for                                of propane acetic acid propylene acrylic acid                                Compound added (%) (%) (%) (%)                                              __________________________________________________________________________    Example 5                                                                          potassium hydro-                                                                       35.0  5.9    3.1    72.6                                           gen carbonate                                                                Example 6 potassium hydro- 48.8 6.5 2.5 68.5                                   gen carbonate                                                                Example 7 diammonium hydro- 31.7 8.9 4.5 63.7                                  gen phoaphate                                                                Example 8 ruhidium nitrat9 29.6 5.4 5.4 68.6                                  Example 9 potassium hydro- 32.1 4.7 4.3 69.5                                   gen carbonate,                                                                diammonium hydro-                                                             gen phosphate                                                              __________________________________________________________________________

In the Examples shown in Table 2, the reaction was conducted at 400° C.,except that the reaction temperature in Example 6 was 420° C.

EXAMPLES 10 AND 11

The oxide "a" obtained in Example 5 was used as a catalyst to react thetest gas under the conditions of an SV of 3,200 (Example 10) or 4,800(Example 11) and a temperature of 400° C. The results obtained are shownin Table 3 below.

                                      TABLE 3                                     __________________________________________________________________________                 Conversion                                                                          Selectivity for                                                                      Selectivity for                                                                      Selectivity for                                Space velocity of propane acetic acid propylene acrylic acid                  (hr.sup.-1) (%) (%) (%) (%)                                                 __________________________________________________________________________    Example 10                                                                          3200   31.9  9.1    5.5    60.8                                           Example 11 4800 22.5 7.2 13.6 61.1                                          __________________________________________________________________________

While the invention has been described in detail and with reference tospecific embodiments thereof, it will be apparent to one skilled in theart that various changes and modifications can be made therein withoutdeparting from the spirit and scope thereof.

What is claimed is:
 1. A process for producing acrylic acid from propaneand oxygen gas through a vapor-phase catalytic oxidation reaction, saidprocess comprising conducting the reaction using as a catalyst a metaloxide containing metallic elements Mo, V, Sb, and A (provided that A isat least one element selected from the group consisting of Nb, Ta, Sn,W, Ti, Ni, Fe, Cr, and Co), said catalyst consisting essentially of Mo,V, Sb and A.
 2. The process for producing acrylic acid as claimed inclaim 1, wherein the metal oxide contains Mo, V, Sb, and A in aproportion represented by the following empirical formula (1):

    MoV.sub.i Sb.sub.j A.sub.k                                 ( 1)

wherein i, j, and k each is from 0.001 to 3.0.
 3. The process forproducing acrylic acid as claimed in claim 1, wherein the amount of theoxygen contained in the catalyst is fixed by the valences of theelements Mo, V, Sb, and A.
 4. A process for producing acrylic acid frompropane and oxygen gas through a vapor-phase catalytic oxidationreaction, said process comprising conducting the reaction using as acatalyst a metal oxide obtained by depositing at least one compoundwhich contains an element B (provided that B is at least one elementselected from the group consisting of Na, K, Rb, Cs, P, and As) as acomponent thereof on a metal oxide which contains metallic elements Mo,V, Sb, and A (provided that A is at least one element selected from thegroup consisting of Nb, Ta, Sn, W, Ti, Ni, Fe, Cr, and Co) and calciningthe resultant mixture, wherein said catalyst consists essentially of Mo,V, Sb, A and B.